EP0029324A1 - Destillationsverfahren zur Abtrennung eines Methankopfproduktes aus einem Gemisch mit einem sauren Gas und die dabei erhaltenen Produkte - Google Patents

Destillationsverfahren zur Abtrennung eines Methankopfproduktes aus einem Gemisch mit einem sauren Gas und die dabei erhaltenen Produkte Download PDF

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EP0029324A1
EP0029324A1 EP80303957A EP80303957A EP0029324A1 EP 0029324 A1 EP0029324 A1 EP 0029324A1 EP 80303957 A EP80303957 A EP 80303957A EP 80303957 A EP80303957 A EP 80303957A EP 0029324 A1 EP0029324 A1 EP 0029324A1
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Prior art keywords
carbon dioxide
methane
column
solids
acid gas
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French (fr)
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EP0029324B1 (de
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Arthur Sherwood Holmes
James Mckee Ryan
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Koch Process Systems Inc
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Koch Process Systems Inc
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B01D3/146—Multiple effect distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B01D3/322—Reboiler specifications
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/20—Use of additives, e.g. for stabilisation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/928—Recovery of carbon dioxide
    • Y10S62/929—From natural gas

Definitions

  • This invention is in the field of cryogenic distillation.
  • carbon dioxide usually must be separated from gas mixtures caused by injecting carbon dioxide- containing gases into oil wells for enhanced oil recovery. Similar separations are often desirable in coal gasification and petrochemical plants. Further, it is sometimes necessary to separate carbon dioxide from hydrogen-rich gas mixtures, such as synthesis gas used for ammonia production.
  • Adsorption by solids has generally been economically . practical, however, only when the feed gas contained relatively small amounts of carbon dioxide and it was required that substantially all of the carbon dioxide be removed. Thus, adsorption processes have-limitations in their application.
  • Chemical absorption systems have generally employed solvents, including amines, such as monoethanolamine and diethanolamine, or carbonates, such as potassium carbonate.
  • Physical absorption systems have employed polar liquid solvents, such as methanol, ethylene glycol, dimethylether, polyethylene glycol, methylpyrrolidone and propylene carbonate.
  • polar liquid solvents such as methanol, ethylene glycol, dimethylether, polyethylene glycol, methylpyrrolidone and propylene carbonate.
  • Such disadvantages include relatively high utility consumption, high maintenance costs due to the corrosive nature of the solvents, and degradation of the solvents by the products separated.
  • the feed gas described contains only about 1% carbon dioxide, it is first treated to remove most of the carbon dioxide before the gas stream is introduced into the low pressure column Because of the diluted carbon dioxide content, the distillation column does not contain a zone of operation where conditions are such that carbon dioxide freeze-out occurs.
  • Harmens in U.S. Patent No. 3,306,057 describes yet another process in which feed gas is reduced to about 11% carbon dioxide in the overhead production of a distillation column. Further carbon dioxide separation is achieved in a heat absorber containing a slurry of solid carbon dioxide in a carrier liquid.
  • a heat absorber containing a slurry of solid carbon dioxide in a carrier liquid.
  • the invention provides a distillative method of separating a methane overhead product from a mixture containing methane and an acid gas component which component is liable to solidify under the distillation conditions, characterised in that an additional liquid component is included 'in the mixture under distillation to prevent solidification of said acid gas component.
  • the acid gas comprises, for example carbon dioxide or hydrogen sulfide, substantially all of which carbon dioxide or hydrogen sulfide may be removed from the overhead methane product.
  • the additional liquid component may be a non-polar liquid which is miscible with methane under the distillation conditions.
  • the component may comprise ethane, propane, butane, pentane or mixtures thereof.
  • the invention also provides a method of separating a methane overhead product from a feed stream containing methane and carbon dioxide, characterised by the steps of a) cooling said feed stream; b) introducing said cooled feed stream into a distillation column having a plurality of vapor-liquid contact stages, said column operating under conditions creating a zone where carbon dioxide is liable to solidify; c) providing sufficient heat at the bottom of said column to provide an enriched methane overhead stream; d) condensing a portion of said methane overhead stream by cooling it and directing it back to the top of said column as reflux; e) withdrawing a methane overhead stream as product; f) withdrawing a bottoms product stream enriched in carbon dioxide from the bottom of said column; and, g) introducing an . additional liquid component into said zone where carbon dioxide is liable to solidify in an amount sufficient to prevent solids formation therein.
  • the invention also provides methane or the acid gas product of a method according to the invention.
  • Embodiments of the invention are described hereinafter by way of example. These embodiments involve the separation of methane from a gas mixture containing methane and one or more acid gas components, such as carbon dioxide, by an improved cryogenic distillative separation. This process is effective for feed gas mixtures which contain relatively high percentages of acid gas components, such as a feed gas mixture containing high carbon dioxide content.
  • the method described is capable of handling feed gases containing low carbon dioxide content and / or additional components besides methane and carbon dioxide. Typical additional components include nitrogen and hydrocarbons of higher molecular weight than methane.
  • a distillation column is used to separate feed gas into an overhead product which is substantially free of acid gas components and a bottoms product substantially free of methane.
  • the distillation column is operated at temperatures, compositions and pressures which produce a solids potential zone for acid gas components within the tower. Such conditions are necessary, in fact, to separate a high C0 2 -content gas if the overhead product gas stream is to contain very low amounts of carbon dioxide.
  • solids potential zone is employed because, as explained below, although conditions in the tower are such that acid gas solids would normally occur, thus interferring with the desired separation, the process described herein prevents actual solids formation from occurring.
  • an additional liquid component for preventing acid gas solids is added to the column so that it is present throughout the solids potential zone.
  • This component can be an external additive, or in the alternative, can be one or more recycled components from the bottoms product taken from the distillation column.
  • the component is added in a sufficient quantity to prevent carbon dioxide or other acid gas components from forming solids in the solids potential zone of the column, thereby allowing a more complete distillative separation of methane from acid gas components to be achieved.
  • cryogenic distillative separation described herein is considered to offer significant advantages over prior distillative processes operated to avoid conditions where acid gas solids occurred, as well as advantages over physical and chemical absorption systems.
  • One advantage, for example, is that a more complete . distillative separation of methane from acid gas ' components is possible in one column. This is in contrast to prior separations requiring a multi-column system or a system having one or more distillation columns together with preseparation apparatus to remove most of the acid gas components prior to admitting the feed gas to the column,
  • the distillative separation described herein is also cost effective, particularly for high-carbon dioxide feed streams. In fact, less energy is required to be supplied for high carbon dioxide content gases with this method than with many of the prior art absorption processes. Capital investment can also be lower since additional columns or carbon dioxide pre- separation apparatus is not required.
  • a potential by-product of subsequent bottoms product separation from a feed containing methane and carbon dioxide is high-purity pressurized carbon dioxide.
  • This pressurized high-purity product is not provided with many of the competing separation processes commercially available, such as chemical or physical absorption.
  • Natural gas liquids are another by-product which can be conveniently achieved with this cryogenic distillative separation if they are present in the feed.
  • NGL Natural gas liquids
  • Figure 1 is a vapor-liquid-solid phase diagram for the methane/carbon dioxide binary system at 650 psia.
  • Figure 1 is a vapor-liquid-solid phase diagram for the methane/carbon dioxide binary system at 650 psia.
  • actual data points for the binary system are not shown, but the data employed to make the plot were based upon data taken from Donnelly, H.G. and Katz, D.L., Ind. Eng. Chem., 46, 511 (1954).
  • the methane/carbon dioxide binary system at 650 psia contains areas of liquid only, vapor only, vapor and liquid in coexistence and areas in which solids coexist with either liquid or vapor.
  • the solids are caused by freeze-out of carbon dioxide at certain conditions.
  • Experimental data from other sources indicate that solid carbon dioxide formation occurs over a broader range of conditions than shown in Fig. 1, which would be even more disadvantageous in an attempted cryogenic distillative separation.
  • feed streams already low in carbon dioxide e.g., less than about 9% can be further separated in a system at 650 psia without encountering solids formation.
  • feeds which are relatively high in carbon dioxide and which need to be separated into methane products having most of the carbon dioxide removed which present the problems.
  • Fig. 2 illustrates the problems encountered in attempting to obtain substantially complete separations of carbon dioxide from methane by a cryogenic distillation in one tower from another perspective.
  • Fig. 2 is a plot of liquid compositions present on trays in a distillative separation of a binary methane/ carbon dioxide feed in columns operated at 500, 600 and 715 psia.
  • the solids potential zone for carbon dioxide is the area to the left of the line representing the carbon dioxide solubility limits in the pure binary system. Solubility data are from Cheung, H. and Zander, E.H., CEP Symposium Series No. 88, Vol. 64 (1968) and Kurata, F., ATChE J. Vol. 8, No. 4, (1964).
  • the 500 and 600 psia data were obtained from computer simulations using a plate-to-plate column calculation program named the PROCESS SM Simulation Program, June-July 1979, which is available from Simulation Sciences, Inc., Fullerton, Cal.
  • the 715 psia data were taken directly from Trentham et al., U.S. Patent No. 4,152,129.
  • a carbon dioxide solids zone exists between liquids containing about 6-7% carbon dioxide to about 80% carbon dioxide.
  • the range is from about 9% to about 65% carbon dioxide. Since liquid compositions within both of these ranges are present in a cryogenic distillative separation of a binary of 50% carbon dioxide/50% methane, solids will be encountered. Once through the solids formation zone, very complete separations are possible. Once again, it can be seen that the problem of solids formation is not present if the liquid composition is relatively low in carbon dioxide, i.e., below about 6-7% at 500 psia and below about 9% at 600 psia.
  • Fig. 2 also indicates that the 715 psia line misses the solids formation zone. Such a high pressure, however, approaches critical pressure of the mixture at the column top which limits the separation which can be achieved and makes design and/or operation of a distillation tower difficult and impractical.
  • Fig 3. is a plot of data illustrating the solubility of carbon dioxide at various temperatures in pure methane and in methane-butane mixtures containing 10%, 20% and 30% butane, respectively.
  • the liquid phase has the indicated percent butane and the percent carbon dioxide is indicated on the ordinate.
  • the balance is methane.
  • butane one preferred solids-preventing agent, is illustrated.
  • the addition of butane substantially increases the solubility of carbon dioxide and decreases the freezing temperature.
  • as much as 10-15°F extra latitude can be gained by the addition of butane.
  • Fig. 4 is a plot of data illustrating the . solubility of hydrogen sulfide, another acid gas, at various temperatures in binary mixtures of hydrogen sulfide and each of the light hydrocarbons, methane, propane and n-butane. As can be seen, the solubility of H 2 S is significantly larger in propane and butane than in methane.
  • dry feed gas 10 containing a mixture of methane and carbon dioxide, and usually other components such as nitrogen and higher alkanes, enters in inlet feed line 12.
  • the feed gas is initially cooled in pre-cooler 14 and subsequently cooled to cryogenic temperatures in heat exchanger 16 which receives refrigeration from refrigeration source 17.
  • heat exchanger 16 which receives refrigeration from refrigeration source 17.
  • cryogenically cooled feed is introduced onto one or more of the trays in distillation column 18.
  • Distillation column 18 contains a number of vapor-liquid.contact stages, such as trays or packing, with the exact number of contact stages depending upon the required operating conditions, of course.
  • Purified methane is withdrawn in overhead line 20 and passed through partial condenser 22.
  • Product s methane is withdrawn in line 24 and passes through pre-cooler 14.
  • Condenser 22 receives refrigeration from refrigeration source 26 and provides reflux in line 23 to tower 18. In some systems, of course, a condenser is not employed.
  • the balance of the bottoms product passes through line 36 to further separation equipment 38 for separating out other fractions, such as an ethane plus fraction separated and collected through line 40.
  • a carbon dioxide fraction is extracted through line 42.
  • recycled solids-preventing agent can be directed through flow control valve 52 into line 54 and added to dry feed gas 10 via valve 56 in line 58 at a point immediately prior to exchanger 16, or through flow control valve 60 and line 62 at a point prior to pre-cooler 14. In some cases where there is a problem with potential solids formation at the point in which dry feed gas 10 enters the column, such recycled agent is desirable.
  • recycled solids-preventing agent in line 50 can be directed through flow control valve 64 and line 66 to an elevated point in column 18.
  • a still further alternative is to add recycled agent via flow control valve 68 and line 70 to the uppermost stage in column 18.
  • Still yet another alternative point at which recycled agent can be added is to condenser 22 via flow control valve 72 and flow line 74.
  • solids-preventing agent can be an externally added agent.
  • solids-preventing agent can be added externally via line 76 and flow control valve 78 to any of the locations previously described for recycled agent.
  • solids-preventing agent is used herein merely as a convenience to describe the class of additives which prevent formation of solid carbon dioxide or other acid gas components in the solids potential zone.
  • the specific mechanism by which such agents operate to prevent solids formation is not entirely understood. It may relate to increased solubility for acid gas components, but it is clear that such additives provide other advantages, some of which are described below.
  • any material or mixture of materials which prevents acid gas solids from forming in the solids potential zone are satisfactory as solids-preventing agents.
  • Nonpolar liquids which are misciblo with methane, such as C 3 -C 6 alkanes, are preferred agents because they are typically present in feed gases, are easy to separate and recycle, and seem to have a beneficial effect on moving the system operating conditions away from critical conditions by raising the critical temperature and pressure of the system.
  • Certain natural gas liquids (NGL) contain such alkanes and can often be separated from s bottoms product in conventional separation equipment. Thus, these NGL or components thereof can be conveniently recycled. It is also clear that materials satisfactory for solids-preventing agent need not be pure materials.
  • the solids-preventing agents should be liquid at the overhead temperature in the distillation column. It is desirable, of course, to have solids-preventing agents which have volatilities lower than carbon dioxide or other acid gases.
  • the agent should also have a freezing point lower than this temperature to avoid solids formation of agent. For example, in a column operating at 600 psia and producing a relatively pure methane product, the temperature at the overhead will be about -130°F, and so candidate agents should have a freezing point below this temperature. At other pressures, different overhead temperatures will be present.
  • the amount of agent added will be dependent upon factors such as e.g. the composition of the feed, operating pressure, throughput of the column, desired purity of overhead methane. Such factors can be taken into account by those skilled in the art by determining the operative amounts for any given separation using no more than routine experimentation.
  • factors such as e.g. the composition of the feed, operating pressure, throughput of the column, desired purity of overhead methane.
  • Such factors can be taken into account by those skilled in the art by determining the operative amounts for any given separation using no more than routine experimentation.
  • amounts of n-butane used as solids-preventing agent ranging from about 0.05 moles to 0.30 moles agent per mole of feed are suitable. Since addition of the agent also sometimes increases carbon dioxide solubility, it is believed that amounts even lower than those calculated can be employed.
  • n-Butane was then added as a solids-preventing agent to the binary methane/carbon dioxide mixture and the conditions within the tower were calculated for 500 psia.
  • the program converged.
  • Table 1 and Fig. 6 illustrate that when butane was added only to the condenser, the condenser temperature increased by up to about 20°F when 320 moles per hour of butane were added. The reduced temperature (actual temperature/critical temperature) of the reflux also moved well away from criticality. Butane losses in the overhead were satisfactorily low.
  • a solid line has been drawn to indicate the lowest solubility of carbon dioxide which was found from solubility data of carbon dioxide in the following six systems: C 1 -CO 2 ; C 2 -C0 2 ; C 3 -CO 2 ; C 1 -CO 2 -C 3 ; C 1 -CO 2 -C 3 ; and CI - C02 - C2 - C3 .
  • Data for these systems were obtained from Kurata, "Solubility of Solid Carbon Dioxide in Pure Light Hydrocarbons and Mixtures of Light Hydrocarbons", Research Report 10, Gas Processors Association, (Feb., 1974).
  • tray 2 remained in the potential freezing region as predicted by the line of lowest solubility even when 320 moles/ hour butane for 2,000 moles/hour of 50/50 methane/carbon dioxide feed was employed. It should be further noted, however, that the runs utilizing both 160 and 320 moles/ hour of butane were outside the zone of freezing for a butane-containing system.
  • the embodiments of the invention are useful in the cryogenic distillative separation of methane from mixtures containing methane and relatively high amounts of carbon dioxide and/or other acid gas components, as well as in other cryogenic distillative separations, such as the separation of methane from ethane.
EP80303957A 1979-11-14 1980-11-06 Destillationsverfahren zur Abtrennung eines Methankopfproduktes aus einem Gemisch mit einem sauren Gas und die dabei erhaltenen Produkte Expired EP0029324B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US06/094,226 US4318723A (en) 1979-11-14 1979-11-14 Cryogenic distillative separation of acid gases from methane
US94226 1979-11-14

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EP0029324A1 true EP0029324A1 (de) 1981-05-27
EP0029324B1 EP0029324B1 (de) 1984-05-23

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US (1) US4318723A (de)
EP (1) EP0029324B1 (de)
JP (1) JPS56501690A (de)
AT (1) ATE7627T1 (de)
AU (1) AU537308B2 (de)
CA (1) CA1124169A (de)
DE (1) DE3067964D1 (de)
IN (1) IN153893B (de)
MX (1) MX155577A (de)
NO (1) NO151800C (de)
NZ (1) NZ195313A (de)
WO (1) WO1981001459A1 (de)

Cited By (3)

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US4318723A (en) 1982-03-09
AU6642381A (en) 1981-06-03
EP0029324B1 (de) 1984-05-23
NO151800C (no) 1985-06-05
CA1124169A (en) 1982-05-25
MX155577A (es) 1988-03-29
JPS56501690A (de) 1981-11-19
NO812326L (no) 1981-07-08
AU537308B2 (en) 1984-06-14
ATE7627T1 (de) 1984-06-15
WO1981001459A1 (en) 1981-05-28
IN153893B (de) 1984-08-25
NO151800B (no) 1985-02-25
DE3067964D1 (en) 1984-06-28
NZ195313A (en) 1983-04-12

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